A device, process, and catalyst intended for desulfurization and demercaptanization of gaseous hydrocarbonsd

ABSTRACT

This application is in the field of technologies for desulfurization and demercaptanization of gaseous hydrocarbons. The device includes a catalytic reactor loaded with a catalyst solution in an organic solvent, a means of withdrawal sulfur solution from the reactor into the sulfur-separating unit, and a sulfur-separating unit. The said device has at least means of supplying gaseous hydrocarbon medium to be purified and oxygen-containing gas into the reactor, and a means of outletting the purified gas from the reactor. The sulfur-separation unit includes a means of sulfur extraction. The reactor design and the catalyst composition provide conversion of at least 99.99% of hydrogen sulfide and mercaptans into sulfur and disulfides. The catalyst is composed of mixed-ligand complexes of transition metals. The technical result achieved by use of claimed invention is single-stage purification of gaseous hydrocarbons from hydrogen sulfide and mercaptans with remaining concentration of —SH down up to 0.001 ppm.

CROSS-REFERENCE TO RELATED APPLICATIONS

The present application is a National stage application from the PCT application PCT/RU2016/000415 filed on Jul. 7, 2016 which claims priority to Russian application RU2016116049 filed on Apr. 25, 2016.

FIELD OF INVENTION

This application is in the field of technologies for desulfurization and demercaptanization of raw gaseous hydrocarbons (including natural gas, tail gas, technological gas, etc). It can be used for desulfurization and demercaptanization of any kind of raw gaseous hydrocarbons.

BACKGROUND

A prior art (RU patent No. 2,394,635, issued on Jul. 20, 2010) discloses a process for desulfurization and demercaptanization of gas based on absorption method. The gases to be purified are pressurized, and treated by two absorbing agents, first by water solution of neutral sodium salts of hydrosulfuric acid and of carbonic acid, and then by water solution of sodium hydroxide.

The same prior art describes a device for desulfurization and demercaptanization of gas as well as removal of carbon dioxide and other acidic additives, that includes two absorbers, each of them includes a storage vessel to hold absorbing agent and a pump that provides metered flow of absorbing agent into the absorber, where the second absorber, relatively to gas flow direction, contains solution of sodium hydroxide, and exhaust collecting vessels to collect exhaust absorbing agents. The absorbers are connected in a cascade; they are pressurized; the second absorber is equipped with a circulation pump; the exhaust collecting vessel of the first absorber is connected with a charging pump that is used to dump exhaust absorbing agent into isolated chambers, where as an absorbing agent in the first absorber, water and exhaust absorbing agent from the second absorber are used; additionally, the said device includes a compressor that maintains required pressure of the gas to be purified, and a separator that is connected to the said compressor, that is used to remove gas condensate and water.

Due to the disadvantages of the said prior art, the following must be admitted: low purification performance, high alkali discharge rate, generation of a high amount of toxic waste that is hard to dispose of.

A prior art (U.S. Pat. No. 4,622,212, issued on Nov. 11, 1986) describes a process of liquid-state oxidation of hydrogen sulfide to sulfur by means of chelating complexes of iron (Lo-Cat process). In the Lo-Cat process, a catalytic reactor for conversion of hydrogen sulfide into sulfur is used, and a device to regenerate the catalyst solution.

The said process features insufficient degree of desulfurization and incapability of demercaptanization that must be admitted as its disadvantages.

A prior art (U.S. Pat. No. 8,735,316, issued on May 27, 2014) describes a process of catalytic demercaptanization by converting mercaptans to disulfides. As a catalyst, the complex CuCl with monoethanol amine (MEA), acetonitrile, or with a monobasic alcohol is used. The process flows in presence of air oxygen, at a temperature of 22-140° C. The residual amount of mercaptan sulfur can be reduced to 20 ppm.

The said process is capable of purifying only liquid media, and no data is provided concerning its capability of hydrogen sulfide removal, that must be admitted as the disadvantages of the previous invention.

A prior art (RU patent No. 2,385,180 issued on Mar. 27, 2010) describes a Claus-process of obtaining sulfur from hydrogen sulfide by means of catalytic reaction of hydrogen sulfide and sulfur dioxide.

The previous invention features primary amine treatment of the, multiple stages of the process and insufficient conversion of hydrogen sulfide to sulfur, necessity of tail gas treatment, sophisticated technological equipment, and incapability of demercaptanization, all these items must be admitted as the drawbacks.

A prior art (U.S. Pat. No. 5,286,697, issued on Feb. 15, 1994) also describes an improved Claus process.

The previous invention is also incapable of demercaptanization, and it is less efficient in hydrogen sulfide conversion.

A prior art (RU patent No. 2,405,738, issued on Apr. 27, 2010) describes a means of sulfur recovery from industrial gases by means of a catalyst that contains on dehydroxylated silica gel (97.65% by mass) impregnated with ferric phosphate (III) (2.35%), that provides sulfur formation from hydrogen sulfide.

The said art features insufficient conversion of hydrogen sulfide, and catalyst production complexity, that must be admitted as drawbacks.

A prior art (RU patent No. 2,398,735, issued on Sep. 9, 2010) describes a means of gas desulfurization by oxidizing hydrogen sulfide to elemental sulfur in liquid state in presence of a catalyst, which contains a compound of a transition metal and an organic complexing agent. To oxidize hydrogen sulfide, it is proposed to use air oxygen as oxidizer; as a compound of transition metal, cupric halogenide is used, where the amount of copper in the solution is 0.015 to 0.1% by weight, and where as an organic complexing agents, one of the following is used: dimethylformamide, pyrrolidone, methylpyrrolidone, pyridine, or quinolone; the process flows in a solvent that is taken as one of the following: monobasic alcohol, polybasic alcohol, water, or their mixtures, kerosene, isooctane, gas condensate at temperature of 20-40° C.

The disadvantage of the said process is its mediocre efficiency.

SUMMARY

The technical problem that is solved by means of the proposed invention is to develop an engineering solution that provides desulfurization and demercaptanization with conversion over 99.999%.

The technical result achieved by use of the proposed engineering solution is a single-stage desulfurization/demercaptanization with residual amount of —SH down to 0.001 ppm while producing no toxic waste.

To achieve said technical result, it is proposed to use a device (FIG. 1) and means (FIG. 2) for desulfurization and demercaptanization of gaseous hydrocarbons, and a catalyst for efficient use of the said means. The proposed device includes a catalytic reactor loaded with a catalyst for H₂S and RSH oxidation into sulfur and disulfides respectively in an organic solvent, an apparatus for withdrawal sulfur solution from the reactor to sulfur separation block, and a sulfur separation block, where the device includes at least a means of supplying gas to be purified and oxygen-containing gas into the reactor, a means of outputting the purified gas from the reactor; and where the sulfur separation block includes a means of sulfur segregation; and where the reactor design and catalyst composition provides conversion of at least 99.99% of hydrogen sulfide and mercaptans to sulfur and disulfides; and where the catalyst is composed of mixed-ligand complexes of transition metals.

While the gas is passed through the catalyst solution, hydrogen sulfide and mercaptans are converted into sulfur and disulfides in accordance with reaction:

H₂S+2RSH+O₂=S+RSSR+2H₂O  (1)

The purified gas is given out to the end user from reactor outlet. The disulfides formed in reaction (1) remain in the reactor, and they do not affect the main process in any way. The water that evolves in reaction (1) is partially withdrawn from the reactor together with the purified gas, and partially—with fine sulfur suspension.

Fine sulfur suspension is withdrawn from the reactor into sulfur-separating unit. The sulfur-separation unit may include a means of sulfur separation from the solution with solution recycling into the reactor thereafter.

The device may additionally include a unit for homogenization of mixture of the gas to be purified with the oxygen-containing gas.

The reactor should preferably include a means of distribution of the supplied gas to be purified in the volume of the reactor, or filling plates.

The device may additionally include a means of metered supply of the catalyst.

As a catalyst, the device should preferably use mixed-ligand complexes based on ferric and/or cupric halogenides.

To achieve stated technical result, the developed process of purification of gaseous hydrocarbons from hydrogen sulfide and mercaptans may also be used.

According to the developed process, the raw gas to be purified is mixed with the oxygen-containing gas and passed through the reactor with organic solution of the catalyst that provides conversion of at least 99.99% of hydrogen sulfide and mercaptans into sulfur and disulfides, and where the catalyst is mixed-ligand complexes of transition metals.

The temperature in the device is preferably to be kept in range of 20-140° C.

In the described process implementation, typically the amount of oxygen is taken not less than 50% of total amount of hydrogen sulfide and mercaptan sulfur.

The gas mixture supplied into the reactor is preferably to be evenly distributed in the reactor volume.

In the described process implementation, typically metered supply of the catalyst into the device is used, while the sulfur is separated from the suspension, and the solution is recycled into the reactor.

Typically, a catalyst is used that consists of mixed-ligand complexes of ferric and/or cupric halogenides.

Moreover, in order to achieve the stated technical result it is suggested to use the catalyst for desulfurization and demercaptanization of gaseous hydrocarbons that has the proposed composition. The said catalyst is a 0.0001-100% solution of ferric chloride and/or cupric chloride, amine, and amide, taken in a ratio of 1:20-1:0.1, in alcohol.

In the catalyst, preferably as amines, benzyl amine, cyclohexilamine, pyridine, and as amide-dimethylformamide are used.

BRIEF DESCRIPTION OF DRAWINGS

FIG. 1 shows the block diagram of the proposed device in the most appropriate composition, where the following notations are used: inlet pipe 1 that supplies raw medium to be purified, mixing unit 2 that mixes hydrocarbon gas to be purified with oxygen-containing gas, inlet pipe 3 that supplies oxygen-containing gas, agitator 4 of oxygen-containing gas discharge, pipe 5 that supplies mixture of hydrocarbon gas to be purified with oxygen-containing gas, catalytic reactor 6, means 7 of distribution of mixture of hydrocarbon gas and oxygen-containing gas in the volume of reactor 6 or filling plates, tank 8 containing catalyst solution, agitator 9 of metered supply of catalyst solution from tank 8 into reactor 6, pipe 10 that supplies catalyst solution into reactor 6, pipe 11 that outlets purified gas, pipe 12 that outlets sulfur suspension into sulfur-separating unit 13, pipe 14 of sulfur outlet from sulfur-separating unit 13, pipe 15 that outlets catalyst solution from sulfur-separating unit 13 into catalytic reactor 6 after sulfur has been separated, agitator 16 of catalyst solution recycling from sulfur-separating unit 13 into catalytic reactor 6.

The general stages or the process realization are shown in FIG. 2, where the following notation is used: supplying raw hydrocarbon material mixed with oxygen-containing gas to the reactor—17, passing the raw material through the reactor containing organic solution of the catalyst—18, output of pure gas from the reactor, where the conversion of hydrogen sulfide and mercaptans to sulfur and disulfides is 99.99%—19, usage of oxygen, not less than 50% of total amount of hydrogen sulfide and mercaptan sulfur—20, distribution of gas mixture evenly in the reactor volume—21, metered supply of the catalyst into the reactor—22, separation of sulfur from the suspension and recycling of catalyst solution into the reactor—23, maintaining of temperature in the device in range of 25-140° C.—24.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT

As an agitator of oxygen-containing gas discharge, an air compressor can be used, as an agitator of catalyst solution supply from the tank—a metering pump, and as an agitator of catalyst solution recycling from sulfur-separating unit—whereby a regular pump can be used.

Below, the essence and advantages of the developed technical solution are discussed in examples of practical implementation.

-   -   a. Example 1. Synthesis of catalyst C1. Into a retort, at a room         temperature, 10 ml of ethyl alcohol, 100 ml of octane, 0.2-1 g         of CuCl₂.2H₂O and 0.5-3 g of amine (benzylamine, cyclohexamine,         pyridine) are put. The contents of the retort are mixed until         cupric chloride dissolves completely. This composition of the         catalyst is disclosed in (RU, patent No. 2405738, issued 27 Apr.         2010).     -   b. Example 2. Synthesis of catalyst C2. Into a retort, at a room         temperature, 100 ml of ethyl alcohol, 20 ml of water, 20 ml         (0.25 moles) of dimethylformamide (DMFA), and 15 g (0.09 moles)         of CuCl₂.2H₂O are put. The contents of the flask are mixed until         cupric chloride dissolves completely. This composition of the         catalyst is known from (RU, patent No. 2398735, issued 10 Sep.         2010), however, even before the scientific research being a         basis of current invention was finished, no data on         demercaptanization capabilities of the said catalyst had been         known.

Example 3. Synthesis of catalyst C3. Into a retort, at a room temperature, 100 ml of alcohol, 8-60 g of amine-dimethylformamide (DMFA) mixture, 1.5-14 g of CuCl₂.2H₂O are put. The contents of the flask are mixed until copper chloride dissolves completely.

-   -   a. Example 4. Gas purification involving catalyst C1. The gas is         purified with use of the device and the process that are claimed         as the current invention, but C1 known from (RU, patent No.         2405738, issued 27 Apr. 2010) is used as the catalyst.     -   b. Non-aqueous organic solvent and catalyst C1 synthesized as in         Example 1 are put into the reactor. The gas supplied into the         reactor contains 0.1% vol. of hydrogen sulfide, 0.05% of         mercaptan sulfur and 0.06% vol. of oxygen. The solution         temperature is 25° C. The output gas contains, according to         potentiometric titration results, 40 ppm and 50 ppm of hydrogen         sulfide and mercaptan respectively. Conversion of hydrogen         sulfide and mercaptan is 95.5 and 91% respectively.     -   c. Thus the device and the process claimed as the current         invention even with use of a known catalyst composition (known         from RU, patent No. 2405738, issued 27 Apr. 2010) provide         conversion rate of hydrogen sulfide and mercaptan into sulfur         and disulfides not more than 95.5%.

Example 5. Gas purification in accordance with current invention claim using catalyst C2. Non-aqueous organic solvent and catalyst C2 are put into the reactor. The gas supplied into the reactor contains 1% vol. of hydrogen sulfide, 0.05% SH and 0.5025% vol. of oxygen. The solution temperature is 25° C. The output gas contains, according to potentiometric titration results, 60 ppm of hydrogen sulfide and 60 ppm of mercaptan. Conversion of hydrogen sulfide and mercaptane is 99.4ϰ88% respectively.

-   -   a. Thus examples 4 and 5 illustrate that even using of         non-optimal catalyst composition the device and process claimed         as current invention provide hydrogen sulfide conversion of         95.5-99.4% and mercaptan conversion of 88-91%.

Examples 6-14. Gas purification using catalyst C3 that utilizes the proposed process, catalyst and device.

Non-aqueous organic solvent ant catalyst C3 with content of 0.001-100% are placed into the reactor. The gas supplied into the reactor contains 0.1-1.8% vol. of hydrogen sulfide, 0.05-0.5% of mercaptans and 0.075-1.15% vol. of oxygen. The solution temperature is 20-40° C. The output gas according to potentiometric titration contains 10-0.001 ppm of hydrogen sulfide and 0.001-20 ppm of mercaptans. The conversion of hydrogen sulfide is 99.8-99.9999%, of mercaptan—98-99.9999%. The experiment results with use of different catalysts C1-C3 are shown in Table 1.

TABLE 1 [H₂S] [RSH] content, % mas. in, % out, in, % out, No catalyst amine + amide Cu + Fe vol. ppm vol ppm 4 C1 93 7 0.1 40 0.05 50 5 C2 56 44 1 60 0.05 60 6 C3 60 40 1 10 0.05 10 7 C3 70 30 1 10 0.05 10 8 C3 80 20 1.8 8 0.05 10 9 C3 85 15 0.5 4 0.05 10 10 C3 94 6 0.5 3 0.1 10 11 C3 93 7 1.0 2 0.5 4 12 C3 92 8 1.0 2 0.5 3 13 C3 91 9 1.0 0.01 0.5 0.01 14 C3 90 10 0.1 0.001 0.1 0.001

In frame of current work, the following results were discovered:

Using catalyst C1 with device and process claimed as current invention provide insufficient conversion of hydrogen sulfide and mercaptans, 95.5% and 91% respectively.

Using catalyst C2 with device and process claimed as current invention provides not only desulfurization as in U.S. Pat. No. 2,398,735, issued 10 Sep. 2010, but also demercaptanization. Mercaptan conversion proves to be 88%.

The catalyst proposed in current application catalyzed oxidation of both hydrogen sulfide and mercaptans with high degree of conversion, see Table 2.

Conversion of hydrogen sulfide and mercaptans in Examples 6-14 is shown in Table 2.

TABLE 2 No conversion, % 6 7 8 9 10 11 12 13 14 H₂S 99.0 99.9 99.96 99.8 99.9 99.9 99.98 99.999 99.9999 RSH 98.0 98.0 98.0 98.0 99.8 99.9 99.9 99.99 99.9999

Results of gas purification by proposed process and with proposed device and catalyst C3 with different ratio of amine/amide/transition metal are shown in Table 3. The conditions of experiment are similar to those of experiments No. 6-14.

TABLE 3 [H₂S] [RSH] Content, % mas. in, out, in, out, No catalyst amine amide metal % vol. ppm % vol. ppm 15 C3 89 10 1 1 10 0.1 10 16 C3 45 50 5 1 10 0.1 10 17 C3 40 50 10 1 4 0.1 6 18 C3 10 70 20 1 4 0.1 6

Results of gas purification by proposed process and with proposed device and catalyst C3 in various solvents with ratio of amine/amide/transition metal=4:5:1 are shown in Table 4. The conditions of experiment are similar to those of experiments No. 6-14.

TABLE 4 [H₂S] [RSH] in, out, in, out, catalyst solvent % vol. ppm % vol. ppm C3 octane 1 4 0.1 6 C3 naphtha 1 10 0.1 10 C3 petrol 1 10 0.1 10

Results of gas purification by proposed process and with proposed device, with different content of catalyst C3 are shown in Table 5. The conditions of experiment are similar to those of experiments No. 6-14.

TABLE 5 [H₂S] [RSH] No [C3], % vol. in, % vol. out, ppm in, % vol. out, ppm 19 0.001-0.5  1 10 0.1 12 20 1-5 1 4 0.1 6 21 10 1 0.001 0.1 0.01

Results of gas purification where the gas has different content of methane, ethane, C₃₊ by proposed process and with proposed device and catalyst C3 are shown in Table 6. The conditions of experiment are similar to those of experiments No. 6-14.

TABLE 6 content, [H₂S] [RSH] % vol. in, out, in, out, No catalyst C₁ C₂ C₃₊ % vol. ppm % vol. ppm 22 C3 85 12 3 1 10 0.1 10 23 C3 74 22 4 1 10 0.1 10 24 C3 100 1 10 0.1 10 25 C3 95 5 1 4 0.1 5

The examples provided confirm that the stated technical result is achieved, yet they do not show the limits of proposed technical solution.

It will be understood that the system and method may be embodied in other specific forms without departing from the spirit or central characteristics thereof. The present examples and embodiments, therefore, are to be considered in all respects as illustrative and not restrictive, and the system method is not to be limited to the details given herein. 

What is claimed is: 1-16. (canceled)
 17. A device for desulfurization and demercaptanization of a gaseous hydrocarbon medium, comprising: a catalytic reactor containing an organic solvent of a catalyst for H₂S oxidation and RSH oxidation into sulfur and disulfides respectively, a sulfur-separating unit, a means for withdrawing a sulfur solution from the reactor into the sulfur-separating unit, at least one means for supplying into the reactor a gas to be purified and an oxygen-containing gas, a means for outputting a purified gas from the reactor, wherein the sulfur-separating unit comprises a means for sulfur extraction, wherein a reactor design and a catalyst composition provide for at least a 99.99% conversion of hydrogen sulfide and mercaptans into sulfur and disulfides, and wherein the catalyst comprises mixed-ligand complexes of transition metals.
 18. The device of claim 17, wherein the means for supplying a gas to be purified and an oxygen-containing gas comprises a means for homogenization of a mixture of hydrocarbon gas to be purified and an oxygen-containing gas.
 19. The device of claim 17, wherein the reactor further comprises a means for distribution of a supplied gas flow evenly within the reactor or within one or more filling plates of said device.
 20. The device of claim 17, wherein the device further comprises a means for metered supply of the catalyst.
 21. The device of claim 17, wherein one or more mixed-ligand complexes based on ferric and/or cupric halogenides are used as the catalyst.
 22. The device of claim 17, wherein the sulfur-separating unit comprises a means for sulfur extraction from the sulfur solution and a means for recycling the sulfur solution thereafter.
 23. A process for desulfurization and demercaptanization of gaseous hydrocarbons, comprising: passing a mixture of gaseous hydrocarbons and an oxygen-containing gas through a reactor loaded with an organic solution of a catalyst, wherein a conversion of hydrogen sulfide and mercaptans into sulfur and disulfides is at least 99.99%, and wherein the catalyst comprises mixed-ligand complexes of transition metals.
 24. The process of claim 23, wherein an amount of oxygen is at least 50% of the total amount of hydrogen sulfide and mercaptan sulfur.
 25. The process of claim 23, wherein the mixture supplied into the reactor is distributed evenly within the reactor.
 26. The process of claim 23, wherein the catalyst is supplied into the reactor by a metered supply unit.
 27. The process of claim 23, further comprising: separating sulfur from a suspension comprising catalyst solution and sulfur, and recycling the catalyst solution into the reactor.
 28. The process of claim 23, wherein the temperature inside the reactor is maintained in a range of 25-140° C.
 29. The process of claim 23, wherein the catalyst comprises mixed-ligand complexes based on ferric and/or cupric halogenides.
 30. A catalyst for purification of gaseous hydrocarbons from hydrogen sulfide and/or mercaptans, comprising: a solution comprising a ratio in a range of 0.0001-100% of a mixture of ferric and/or cupric chlorides, amines, and amides, said mixture being dissolved in a ratio of 1:20-1:0.1 in alcohol.
 31. The catalyst of claim 30, wherein the amines are benzylamine, cyclohexylamine, and/or pyridine.
 32. The catalyst of claim 30, wherein the amides are dimethylformamide. 